EP1624000B1 - procédé de polymérisation pour la production de polymères plus faciles à traiter - Google Patents

procédé de polymérisation pour la production de polymères plus faciles à traiter Download PDF

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EP1624000B1
EP1624000B1 EP05024910A EP05024910A EP1624000B1 EP 1624000 B1 EP1624000 B1 EP 1624000B1 EP 05024910 A EP05024910 A EP 05024910A EP 05024910 A EP05024910 A EP 05024910A EP 1624000 B1 EP1624000 B1 EP 1624000B1
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bulky ligand
catalyst
group
type catalyst
metallocene
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EP1624000A1 (fr
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Donna J. Crowther
Ching-Tai Lue
Philip T. Matsunaga
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ExxonMobil Chemical Patents Inc
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ExxonMobil Chemical Patents Inc
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    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07F—ACYCLIC, CARBOCYCLIC OR HETEROCYCLIC COMPOUNDS CONTAINING ELEMENTS OTHER THAN CARBON, HYDROGEN, HALOGEN, OXYGEN, NITROGEN, SULFUR, SELENIUM OR TELLURIUM
    • C07F17/00—Metallocenes
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J31/00—Catalysts comprising hydrides, coordination complexes or organic compounds
    • B01J31/16—Catalysts comprising hydrides, coordination complexes or organic compounds containing coordination complexes
    • B01J31/1608—Catalysts comprising hydrides, coordination complexes or organic compounds containing coordination complexes the ligands containing silicon
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J31/00—Catalysts comprising hydrides, coordination complexes or organic compounds
    • B01J31/16—Catalysts comprising hydrides, coordination complexes or organic compounds containing coordination complexes
    • B01J31/22—Organic complexes
    • B01J31/2282—Unsaturated compounds used as ligands
    • B01J31/2295—Cyclic compounds, e.g. cyclopentadienyls
    • C—CHEMISTRY; METALLURGY
    • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
    • C08F—MACROMOLECULAR COMPOUNDS OBTAINED BY REACTIONS ONLY INVOLVING CARBON-TO-CARBON UNSATURATED BONDS
    • C08F10/00—Homopolymers and copolymers of unsaturated aliphatic hydrocarbons having only one carbon-to-carbon double bond
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2531/00—Additional information regarding catalytic systems classified in B01J31/00
    • B01J2531/02—Compositional aspects of complexes used, e.g. polynuclearity
    • B01J2531/0286—Complexes comprising ligands or other components characterized by their function
    • B01J2531/0288—Sterically demanding or shielding ligands
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2531/00—Additional information regarding catalytic systems classified in B01J31/00
    • B01J2531/40—Complexes comprising metals of Group IV (IVA or IVB) as the central metal
    • B01J2531/48—Zirconium
    • C—CHEMISTRY; METALLURGY
    • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
    • C08F—MACROMOLECULAR COMPOUNDS OBTAINED BY REACTIONS ONLY INVOLVING CARBON-TO-CARBON UNSATURATED BONDS
    • C08F210/00—Copolymers of unsaturated aliphatic hydrocarbons having only one carbon-to-carbon double bond
    • C08F210/16—Copolymers of ethene with alpha-alkenes, e.g. EP rubbers
    • C—CHEMISTRY; METALLURGY
    • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
    • C08F—MACROMOLECULAR COMPOUNDS OBTAINED BY REACTIONS ONLY INVOLVING CARBON-TO-CARBON UNSATURATED BONDS
    • C08F2420/00—Metallocene catalysts
    • C08F2420/09—Cyclic bridge, i.e. Cp or analog where the bridging unit linking the two Cps or analogs is part of a cyclic group
    • C—CHEMISTRY; METALLURGY
    • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
    • C08F—MACROMOLECULAR COMPOUNDS OBTAINED BY REACTIONS ONLY INVOLVING CARBON-TO-CARBON UNSATURATED BONDS
    • C08F4/00—Polymerisation catalysts
    • C08F4/42—Metals; Metal hydrides; Metallo-organic compounds; Use thereof as catalyst precursors
    • C08F4/44—Metals; Metal hydrides; Metallo-organic compounds; Use thereof as catalyst precursors selected from light metals, zinc, cadmium, mercury, copper, silver, gold, boron, gallium, indium, thallium, rare earths or actinides
    • C08F4/60—Metals; Metal hydrides; Metallo-organic compounds; Use thereof as catalyst precursors selected from light metals, zinc, cadmium, mercury, copper, silver, gold, boron, gallium, indium, thallium, rare earths or actinides together with refractory metals, iron group metals, platinum group metals, manganese, rhenium technetium or compounds thereof
    • C08F4/62—Refractory metals or compounds thereof
    • C08F4/64—Titanium, zirconium, hafnium or compounds thereof
    • C08F4/659—Component covered by group C08F4/64 containing a transition metal-carbon bond
    • C08F4/65912—Component covered by group C08F4/64 containing a transition metal-carbon bond in combination with an organoaluminium compound
    • C—CHEMISTRY; METALLURGY
    • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
    • C08F—MACROMOLECULAR COMPOUNDS OBTAINED BY REACTIONS ONLY INVOLVING CARBON-TO-CARBON UNSATURATED BONDS
    • C08F4/00—Polymerisation catalysts
    • C08F4/42—Metals; Metal hydrides; Metallo-organic compounds; Use thereof as catalyst precursors
    • C08F4/44—Metals; Metal hydrides; Metallo-organic compounds; Use thereof as catalyst precursors selected from light metals, zinc, cadmium, mercury, copper, silver, gold, boron, gallium, indium, thallium, rare earths or actinides
    • C08F4/60—Metals; Metal hydrides; Metallo-organic compounds; Use thereof as catalyst precursors selected from light metals, zinc, cadmium, mercury, copper, silver, gold, boron, gallium, indium, thallium, rare earths or actinides together with refractory metals, iron group metals, platinum group metals, manganese, rhenium technetium or compounds thereof
    • C08F4/62—Refractory metals or compounds thereof
    • C08F4/64—Titanium, zirconium, hafnium or compounds thereof
    • C08F4/659—Component covered by group C08F4/64 containing a transition metal-carbon bond
    • C08F4/65916—Component covered by group C08F4/64 containing a transition metal-carbon bond supported on a carrier, e.g. silica, MgCl2, polymer
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
    • Y10S—TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10S526/00—Synthetic resins or natural rubbers -- part of the class 520 series
    • Y10S526/901—Monomer polymerized in vapor state in presence of transition metal containing catalyst
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
    • Y10S—TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10S526/00—Synthetic resins or natural rubbers -- part of the class 520 series
    • Y10S526/943—Polymerization with metallocene catalysts

Definitions

  • the present invention relates to a process for polymerizing olefin(s) to produce polymers having improved processability. Also, the invention is directed to a bulky ligand metallocene-type catalyst compound and catalyst system for use in the polymerization of olefin(s) to produce polymers that are easier to process into various articles of manufacture. In particular, the invention is directed to cyclic bridged bulky ligand metallocene-type catalyst systems, their use in a polymerization process, and products produced therefrom.
  • Processability is the ability to economically process and shape a polymer uniformly. Processability involves such elements as how easily the polymer flows, melt strength, and whether or not the extrudate is distortion free.
  • Typical bulky ligand metallocene-type catalyzed polyethylenes (mPE) are somewhat more difficult to process than low density polyethylenes (LDPE) made in a high pressure polymerization process.
  • LDPE low density polyethylenes
  • mPE's require more motor power and produce higher extruder pressures to match the extrusion rate of LDPE's.
  • Typical mPE's also have lower melt strength which, for example, adversely affects bubble stability during blown film extrusion, and they are prone to melt fracture at commercial shear rates.
  • mPE's exhibit superior physical properties as compared to LDPE's.
  • metallocene catalysts produce polymers having a narrow molecular weight distribution.
  • Narrow molecular weight distribution polymers tend to be more difficult to process.
  • the broader the polymer molecular weight distribution the easier the polymer is to process.
  • a technique to improve the processability of mPE's is to broaden the products' molecular weight distribution (MWD) by blending two or more mPE's with significantly different molecular weights, or by changing to a polymerization catalyst or mixture of catalysts that produce broad MWD polymers.
  • MWD molecular weight distribution
  • U.S. Patent No. 5,281,679 discusses bulky ligand metallocene-type catalyst compounds where the bulky ligand is substituted with a substituent having a secondary or tertiary carbon atom for the producing of broader molecular weight distribution polymers.
  • U.S. Patent No. 5,470,811 describes the use of a mixture of bulky ligand metallocene-type catalysts for producing easy processing polymers.
  • U.S. Patent No. 5,798,427 addresses the production of polymers having enhanced processability using a bulky ligand metallocene-type catalyst compound where the bulky ligands are specifically substituted indenyl ligands.
  • This invention relates to a polymerization process utilizing a bridged bulky ligand metallocene-type catalyst system for producing polymer products that have excellent processability and enhanced physical properties. Also, the invention is directed to improved bridged bulky ligand metallocene-type catalyst compounds having a cyclic bridge, catalyst systems comprising these compounds, and polymerizing processes utilizing these compounds.
  • the preferred polymerization processes are a gas phase or a slurry phase process, most preferably a gas phase process.
  • the invention provides for a process for polymerizing ethylene alone or in combination with one or more other olefin(s) in the presence of an achiral cyclic bridged metallocene-type catalyst compound, even more preferably an achiral cyclic bridged metallocene-type catalyst compound having two substituted bulky ligands and an activator.
  • the cyclic bridged metallocene-type catalyst compound has two bulky ligands only one of which is a substituted bulky ligand.
  • the invention relates to a polymerization process for producing easy processing polymers using a cyclic bridged bulky ligand metallocene-type catalyst system. It has been suprisingly discovered that using the cyclic bridged metallocene-type catalysts of the invention, particularly in a slurry or gas phase polymerization process, produces polymers that have a high Melt Index Ratio (MIR). MIR is simply the ratio of I 21 /I 2 , where I 21 is measured by ASTM-D-1238-F and I 2 known as Melt Index (MI) is measured by ASTM-D-1238-E.
  • MI Melt Index
  • bulky ligand metallocene-type catalyst compounds include half and full sandwich compounds having one or more bulky ligands bonded to at least one metal atom.
  • Typical bulky ligand metallocene-type compounds are generally described as containing one or more bulky ligand(s) and one or more leaving group(s) bonded to at least one metal atom.
  • at least one bulky ligand is ⁇ -bonded to a metal atom, most preferably ⁇ 5 -bonded to the metal atom.
  • the bulky ligands are generally represented by one or more open, acyclic, or fused ring(s) or ring system(s) or a combination thereof.
  • These bulky ligands, preferably ring(s) or ring system(s) are typically composed of atoms selected from Groups 13 to 16 atoms of the Periodic Table of Elements, preferably the atoms are selected from the group consisting of carbon, nitrogen, oxygen, silicon, sulfur, phosphorous, boron and aluminum or a combination thereof.
  • the ring(s) or ring system(s) are composed of carbon atoms such as but not limited to those cyclopentadienyl ligands or cyclopentadienyl-type ligand structures or other similar functioning ligand structure such as a pentadiene, a cyclooctatetraendiyl or an imide ligand.
  • the metal atom is preferably selected from Groups 3 through 15 and the lanthanide or actinide series of the Periodic Table of Elements.
  • the metal is a transition metal from Groups 4 through 12, more preferably 4, 5 and 6, and most preferably the metal is from Group 4.
  • the bulky ligand metallocene-type catalyst compounds of the invention are represented by the formula: L A (R'A x R')L B MQ n (I) where M is a Group 4, 5, 6 transition metal, L A and L B is an unsubstituted or substituted, cyclopentadienyl ligand or cyclopentadienyl-type bulky ligand bonded to M; (R'A x R') is a cyclic bridging group where A is one or more of, or a combination of carbon, germanium, silicon or tin bridging L A and L B , and the two R' 's form a cyclic ring or ring system with A; independently, each Q is a monoanionic ligand, or optionally two Q's together form a divalent anionic chelating ligand; and where n is 0, 1 or 2 depending on the formal oxidation state of M, and x is an integer from 1 to 4 and where the
  • Non-limiting examples of cyclic bridging groups A include cyclo-tri or tetra-alkylene silyl or include cyclo-tri or tetra-alkylene germyl groups, for example, cyclotrimethylenesilyl group or cyclotetramethylenesilyl group.
  • cyclic bridging groups are represented by the following structures:
  • the bulky ligand metallocene-type catalyst compounds of the invention include cyclotrimethylenesilyl(tetramethyl cyclopentadienyl) (cyclopentadienyl) zirconium dichloride, cyclotetramethylenesilyl(tetramethyl cyclopentadienyl) (cyclopentadienyl) zirconium dichloride, cyclotrimethylenesilyl (tetramethyl cyclopentadienyl) (2-methyl indenyl) zirconium dichloride, cyclotrimethylenesilyl(tetramethyl cyclopentadienyl) (3-methyl cyclopentadienyl) zirconium dichloride, cyclotrimethylenesilyl bis(2-methyl indenyl) zirconium dichloride, cyclotrimethylenesilyl(tetramethyl cyclopentadienyl) (2,3,5-trimethyl cyclopen
  • the bulky ligand metallocene-type catalyst compound of the invention is represented by the formula: (C 5 H 4-d R d )(R'A x R')(C 5 H 4-d R d ) M Qg- 2 (II) where M is a Group 4, 5, 6 transition metal, (C 5 H 4-d R d ) is an unsubstituted or substituted, cyclopentadienyl ligand or cyclopentadienyl-type bulky ligand bonded to M, each R, which can be the same or different, is hydrogen or a substituent group containing up to 50 non-hydrogen atoms or substituted or unsubstituted hydrocarbyl having from 1 to 30 carbon atoms or combinations thereof, or two or more carbon atoms are joined together to form a part of a substituted or unsubstituted ring or ring system having 4 to 30 carbon atoms, R'A x R' is a cyclic bridging group,
  • R' is a hydrocarbyl containing a heteroatom, for example boron, nitrogen, oxygen or a combination thereof.
  • the two R"s may be independently, hydrocarbyl, substituted hydrocarbyl, halocarbyl, substituted halocarbyl, hydrocarbyl-substituted organometalloid, halocarbyl-substituted organometalloid, where the two R"s may be joined to form a ring or ring system having from 2 to 100 non-hydrogen atoms, preferably from 3 to 50 carbon atoms; and independently, each Q can be the same or different is a hydride, substituted or unsubstituted, linear, cyclic or branched, hydrocarbyl having from 1 to 30 carbon atoms, halogen, alkoxides, aryloxides, amides, phosphides, or any other univalent anionic ligand or combination thereof; also, two Q's together may form an alkylidene
  • the cyclic bridged bulky ligand metallocene-type catalyst compounds are those where the R substituents on the bulky ligands L A , L B , (C 5 H 4-d R d ) of formulas (I) and (II) are substituted with the same or different number of substituents on each of the bulky ligands.
  • the bulky ligands L A , L B , (C 5 H 4-d R d ) of formulas (I) and (II) are different from each other.
  • the bulky ligands of the metallocene-type catalyst compounds of formula (I) and (II) are asymmetrically substituted.
  • at least one of the bulky ligands L A , L B , (C 5 H 4-d R d ) of formulas (I) and (II) is unsubstituted.
  • the cyclic bridged metallocene-type catalyst compounds of the invention are achiral.
  • ligand metallocene-type catalysts compounds useful in the invention include cyclic bridged heteroatom, mono-bulky ligand metallocene-type compounds. These types of catalysts and catalyst systems are described in, for example, PCT publication WO 92/00333 , WO 94/07928 , WO 91/ 04257 , WO 94/03506 , WO96/00244 and WO 97/15602 and U.S. Patent Nos. 5,057,475 , 5,096,867 , 5,055,438 , 5,198,401 , 5,227,440 and 5,264,405 and European publication EP-A-0 420 436 .
  • the cyclic bridged bulky ligand metallocene-type catalyst compound may be represented by the formula: L c AJMQ n (III) where M is a Group 3 to 10 metal atom or a metal selected from the Group of actinides and lanthanides of the Periodic Table of Elements, preferably M is a Group 4 to 10 transition metal, and more preferably M is a Group 4, 5 or 6 transition metal, and most preferably M is a Group 4 transition metal in any oxidation state, especially titanium; L c is a substituted or unsubstituted bulky ligand bonded to M; J is bonded to M; A is bonded to L and J; J is a heteroatom ancillary ligand; and A is a cyclic bridging group; Q is a univalent anionic ligand; and n is the integer 0,1 or 2.
  • L c , A and J form a fused ring system.
  • L c of formula (III) is as defined above for L A in formula (I)
  • A, M and Q of formula (III) are as defined above in formula (I).
  • the bulky ligand metallocene-type catalyst compound useful in the invention is represented by the formula: (C 5 H 5-y-x R x )(R"A y R")(JR' z-l-y )M(Q) n (L') w (IV) where M is a transition metal from Group 4 in any oxidation state, preferably, titanium, zirconium or hafnium, most preferably titanium in either a +2, +3 or +4 oxidation state.
  • M is a transition metal from Group 4 in any oxidation state, preferably, titanium, zirconium or hafnium, most preferably titanium in either a +2, +3 or +4 oxidation state.
  • a combination of compounds represented by formula (IV) with the transition metal in different oxidation states is also contemplated.
  • L c is represented by (C 5 H 5-y-x R x ) and is a bulky ligand as described above.
  • R 0 means no substituent. More particularly (C 5 H 5-y-x R x ) is a cyclopentadienyl ring or cyclopentadienyl-type ring or ring system which is substituted with from 0 to 4 substituent groups R, and "x" is 0, 1, 2, 3 or 4 denoting the degree of substitution.
  • R is, independently, a radical selected from a group consisting of 1 to 30 non-hydrogen atoms.
  • R is a hydrocarbyl radical or a substituted hydrocarbyl radical having from 1 to 30 carbon atoms, or a hydrocarbyl-substituted metalloid radical where the metalloid is a Group 14 or 15 element, preferably silicon or nitrogen or a combination thereof, and halogen radicals and mixtures thereof.
  • Substituent R groups also include silyl, germyl, amine, and hydrocarbyloxy groups and mixtures thereof.
  • (C 5 H 5-y-x R x ) is a cyclopentadienyl ligand in which two R groups, preferably two adjacent R groups are joined to form a ring or ring system having from 3 to 50 atoms, preferably from 3 to 30 carbon atoms.
  • This ring system may form a saturated or unsaturated polycyclic cyclopentadienyl-type ligand such as those bulky ligands described above, for example, indenyl, tetrahydroindenyl, fluorenyl or octahydrofluorenyl.
  • the (JR' z-l-y ) of formula (IV) is a heteroatom containing ligand in which J is an element with a coordination number of three from Group 15 or an element with a coordination number of two from Group 16 of the Periodic Table of Elements.
  • J is a nitrogen, phosphorus, oxygen or sulfur atom with nitrogen being most preferred.
  • Each R' is, independently, a radical selected from the group consisting of hydrocarbyl radicals having from 1 to 20 carbon atoms, or as defined for R in formula (I) above; the "y” is 1 to 4, preferably 1 to 2, most preferably y is 1, and the "z” is the coordination number of the element J.
  • the J of formula (III) is represented by (JR' z-l-y ).
  • each Q is, independently, any univalent anionic ligand such as halogen, hydride, or substituted or unsubstituted hydrocarbyl having from 1 to 30 carbon atoms, alkoxide, aryloxide, sulfide, silyl, amide or phosphide.
  • Q may also include hydrocarbyl groups having ethylenic unsaturation thereby forming a ⁇ 3 bond to M.
  • two Q's may be an alkylidene, a cyclometallated hydrocarbyl or any other divalent anionic chelating ligand.
  • the integer n may be 0, 1, 2 or 3.
  • the (R"A y R") of formula (IV) is a cyclic bridging group where A is a Group 13 to 16 element, preferably a Group 14 and 15 element, most preferably a Group 14 element.
  • A include one or more of, or a combination of carbon, silicon, germanium, boron, nitrogen, phosphorous, preferably at least one silicon atom.
  • L' a Lewis base such as diethylether, tetraethylammonium chloride, tetrahydrofuran, dimethylaniline, aniline, trimethylphosphine, n-butylamine, and the like; and w is a number from 0 to 3. Additionally, L' may be bonded to any of R, R'or Q and n is 0,1,2 or 3.
  • cyclic bridged bulky ligand metallocene-type catalyst compounds are typically activated in various ways to yield catalyst compounds having a vacant coordination site that will coordinate, insert, and polymerize olefin(s).
  • activator is defined to be any compound or component or method which can activate any of the bulky ligand metallocene-type catalyst compounds of the invention as described above.
  • Non-limiting activators for example may include a Lewis acid or a non-coordinating ionic activator or ionizing activator or any other compound including Lewis bases, aluminum alkyls, conventional-type cocatalysts and combinations thereof that can convert a neutral bulky ligand metallocene-type catalyst compound to a catalytically active bulky ligand metallocene cation.
  • alumoxane or modified alumoxane as an activator, and/or to also use ionizing activators, neutral or ionic, such as tri (n-butyl) ammonium tetrakis (pentafluorophenyl) boron or a trisperfluorophenyl boron metalloid precursor or a trisperfluoronaphtyl boron metalloid precursor that would ionize the neutral bulky ligand metallocene-type catalyst compound.
  • ionizing activators neutral or ionic, such as tri (n-butyl) ammonium tetrakis (pentafluorophenyl) boron or a trisperfluorophenyl boron metalloid precursor or a trisperfluoronaphtyl boron metalloid precursor that would ionize the neutral bulky ligand metallocene-type catalyst compound.
  • Ionizing compounds may contain an active proton, or some other cation associated with but not coordinated to or only loosely coordinated to the remaining ion of the ionizing compound.
  • Such compounds and the like are described in European publications EP-A-0 570 982 , EP-A-0 520 732 , EP-A-0 495 375 , EP-A-500 944 , EP-A-0 277 003 and EP-A-0 277 004 , and U.S. Patent Nos. 5,153,157 , 5,198,401 , 5,066,741 , 5,206,197 , 5,241,025 , 5,384,299 and 5,502,124 and U.S. Patent Application Serial No. 08/285,380, filed August 3, 1994 .
  • activators include those described in PCT publication WO 98/07515 such as tris (2, 2', 2"- nonafluorobiphenyl) fluoroaluminate, which publication is fully incorporated herein by reference.
  • Combinations of activators are also contemplated by the invention, for example, alumoxanes and ionizing activators in combinations, see for example, PCT publications WO 94/07928 and WO 95/14044 and U.S. Patent Nos. 5,153,157 and 5,453,410 all of which are herein fully incorporated by reference.
  • WO 98/09996 incorporated herein by reference describes activating bulky ligand metallocene-type catalyst compounds with perchlorates, periodates and iodates including their hydrates.
  • WO 98/30602 and WO 98/30603 incorporated by reference describe the use of lithium (2,2'-bisphenyl-ditrimethylsilicate)•4THF as an activator for a bulky ligand metallocene-type catalyst compound.
  • methods of activation such as using radiation (see EP-B1-0 615 981 herein incorporated by reference), electro-chemical oxidation, and the like are also contemplated as activating methods for the purposes of rendering the neutral bulky ligand metallocene-type catalyst compound or precursor to a bulky ligand metallocene-type cation capable of polymerizing olefins.
  • one or more bulky ligand metallocene-type catalyst compounds or catalyst systems may be used in combination with one or more conventional-type catalyst compounds or catalyst systems.
  • Mixed catalysts and catalyst systems are described in U.S. Patent Nos. 4,159,965 , 4,325,837 , 4,701,432 , 5,124,418 , 5,077,255 , 5,183,867 , 5,391,660 , 5,395,810 , 5,691,264 , 5,723,399 and 5,767,031 and PCT Publication WO 96/23010 published August 1, 1996 .
  • cyclic bulky ligand metallocene-type catalyst compounds and catalyst systems may be combined with one or more support materials or carriers using one of the support methods well known in the art or as described below.
  • the method of the invention uses a polymerization catalyst in a supported form.
  • a bulky ligand metallocene-type catalyst compound or catalyst system is in a supported form, for example deposited on, bonded to, contacted with, or incorporated within, adsorbed or absorbed in, or on, a support or carrier.
  • support or “carrier” are used interchangeably and are any support material, preferably a porous support material, for example, talc, inorganic oxides and inorganic chlorides.
  • Other carriers include resinous support materials such as polystyrene, functionalized or crosslinked organic supports, such as polystyrene divinyl benzene polyolefins or polymeric compounds, zeolites, clays, or any other organic or inorganic support material and the like, or mixtures thereof.
  • the preferred carriers are inorganic oxides that include those Group 2, 3, 4, 5, 13 or 14 metal oxides.
  • the preferred supports include silica, alumina, silica-alumina, magnesium chloride, and mixtures thereof.
  • Other useful supports include magnesia, titania, zirconia, montmorillonite ( EP-B10511 665 ) and the like.
  • combinations of these support materials may be used, for example, silica-chromium, silica-alumina, silica-titania and the like.
  • the carrier most preferably an inorganic oxide, has a surface area in the range of from about 10 to about 700 m 2 /g, pore volume in the range of from about 0.1 to about 4.0 cc/g and average particle size in the range of from about 5 to about 500 ⁇ m. More preferably, the surface area of the carrier is in the range of from about 50 to about 500 m 2 /g, pore volume of from about 0.5 to about 3.5 cc/g and average particle size of from about 10 to about 200 ⁇ m.
  • the surface area of the carrier is in the range is from about 100 to about 400 m 2 /g, pore volume from about 0.8 to about 3.0 cc/g and average particle size is from about 5 to about 100 ⁇ m.
  • the average pore size of the carrier of the invention typically has pore size in the range of from 10 to 1000 ⁇ , preferably 50 to about 500 ⁇ , and most preferably 75 to about 350 ⁇ .
  • the cyclic bridged bulky ligand metallocene-type catalyst compounds of the invention may be deposited on the same or separate supports together with an activator, or the activator may be used in an unsupported form, or may be deposited on a support different from the supported bulky ligand metallocene-type catalyst compounds of the invention, or any combination thereof.
  • the cyclic bridged bulky ligand metallocene-type catalyst compound of the invention may contain a polymer bound ligand as described in U.S. Patent Nos. 5,473,202 and 5,770,755 , which is herein fully incorporated by reference; the bulky ligand metallocene-type catalyst system of the invention may be spray dried as described in U.S. Patent No.
  • the invention provides for a supported cyclic bridged bulky ligand metallocene-type catalyst system that includes an antistatic agent or surface modifier that is used in the preparation of the supported catalyst system as described in PCT publication WO 96/11960 .
  • the catalyst systems of the invention can be prepared in the presence of an olefin, for example hexene-1.
  • a preferred method for producing the supported cyclic bridged bulky ligand metallocene-type catalyst system is described below and is described in U.S. Application Serial Nos. 265,533, filed June 24, 1994 and 265,532, filed June 24, 1994 and PCT publications WO 96/00245 and WO 96/00243 both published January 4, 1996 .
  • the cyclic bridged bulky ligand metallocene-type catalyst compound is slurried in a liquid to form a metallocene solution and a separate solution is formed containing an activator and a liquid.
  • the liquid may be any compatible solvent or other liquid capable of forming a solution or the like with the cyclic bridged bulky ligand metallocene-type catalyst compounds and/or activator of the invention.
  • the liquid is a cyclic aliphatic or aromatic hydrocarbon, most preferably toluene.
  • the cyclic bridged bulky ligand metallocene-type catalyst compound and activator solutions are mixed together and added to a porous support or the porous support is added to the solutions such that the total volume of the bulky ligand metallocene-type catalyst compound solution and the activator solution or the bulky ligand metallocene-type catalyst compound and activator solution is less than four times the pore volume of the porous support, more preferably less than three times, even more preferably less than two times; preferred ranges being from 1.1 times to 3.5 times range and most preferably in the 1.2 to 3 times range.
  • the mole ratio of the metal of the activator component to the metal of the supported cyclic bridged bulky ligand metallocene-type catalyst compounds are in the range of between 0.3:1 to 1000:1, preferably 20:1 to 800:1, and most preferably 50:1 to 500:1.
  • the activator is an ionizing activator such as those based on the anion tetrakis(pentafluorophenyl)boron
  • the mole ratio of the metal of the activator component to the metal component of the cyclic bridged bulky ligand metallocene-type catalyst is preferably in the range of between 0.3:1 to 3:1.
  • the mole ratio of the metal of the activator component to the metal of the cyclic bridged bulky ligand metallocene-type catalyst compound is in the range of between 0.3:1 to 10,000:1, preferably 100:1 to 5000:1, and most preferably 500:1 to 2000:1.
  • olefin(s), preferably C 2 to C 30 olefin(s) or alpha-olefin(s), preferably ethylene or propylene or combinations thereof are prepolymerized in the presence of the cyclic bridged bulky ligand metallocene-type catalyst system of the invention prior to the main polymerization.
  • the prepolymerization can be carried out batchwise or continuously in gas, solution or slurry phase including at elevated pressures.
  • the prepolymerization can take place with any olefin monomer or combination and/or in the presence of any molecular weight controlling agent such as hydrogen.
  • any molecular weight controlling agent such as hydrogen.
  • the polymerization catalyst is used in an unsupported form, preferably in a liquid form such as described in U.S. Patent Nos. 5,317,036 and 5,693,727 and European publication EP-A-0 593 083 , all of which are herein incorporated by reference.
  • the polymerization catalyst in liquid form can be fed to a reactor as described in PCT publication WO 97/46599 .
  • the cyclic bridged metallocene-type catalysts of the invention can be combined with a carboxylic acid salt of a metal ester, for example aluminum carboxylates such as aluminum mono, di- and tri- stearates, aluminum octoates, oleates and cyclohexylbutyrates, as described in U.S. Application Serial No. 09/113,216, filed July 10, 1998 .
  • a carboxylic acid salt of a metal ester for example aluminum carboxylates such as aluminum mono, di- and tri- stearates, aluminum octoates, oleates and cyclohexylbutyrates, as described in U.S. Application Serial No. 09/113,216, filed July 10, 1998 .
  • the catalysts and catalyst systems of the invention described above are suitable for use in any polymerization process over a wide range of temperatures and pressures.
  • the temperatures may be in the range of from -60 °C to about 280°C, preferably from 50°C to about 200°C, and the pressures employed may be in the range from 1 atmosphere to about 500 atmospheres or higher.
  • Polymerization processes include solution, gas phase, slurry phase and a high pressure process or a combination thereof. Particularly preferred is a gas phase or slurry phase polymerization of one or more olefins at least one of which is ethylene or propylene.
  • the process of this invention is directed toward a solution, high pressure, slurry or gas phase polymerization process of one or more olefin monomers having from 2 to 30 carbon atoms, preferably 2 to 12 carbon atoms, and more preferably 2 to 8 carbon atoms.
  • the invention is particularly well suited to the polymerization of two or more olefin monomers of ethylene, propylene, butene-1, pentene-1, 4-methyl-pentene-1, hexene-1, octene-1 and decene-1.
  • monomers useful in the process of the invention include ethylenically unsaturated monomers, diolefins having 4 to 18 carbon atoms, conjugated or nonconjugated dienes, polyenes, vinyl monomers and cyclic olefins.
  • Non-limiting monomers useful in the invention may include norbornene, norbornadiene, isobutylene, isoprene, vinylbenzocyclobutane, styrenes, alkyl substituted styrene, ethylidene norbornene, dicyclopentadiene and cyclopentene.
  • a copolymer of ethylene is produced, where with ethylene, a comonomer having at least one alpha-olefin having from 4 to 15 carbon atoms, preferably from 4 to 12 carbon atoms, and most preferably from 4 to 8 carbon atoms, is polymerized in a gas phase process.
  • ethylene or propylene is polymerized with at least two different comonomers, optionally one of which may be a diene, to form a terpolymer.
  • the invention is directed to a polymerization process, particularly a gas phase or slurry phase process, for polymerizing propylene alone or with one or more other monomers including ethylene, and/or other olefins having from 4 to 12 carbon atoms.
  • Polypropylene polymers may be produced using the particularly bridged bulky ligand metallocene-type catalysts as described in U.S. Patent Nos. 5,296,434 and 5,278,264 .
  • a continuous cycle is employed where in one part of the cycle of a reactor system, a cycling gas stream, otherwise known as a recycle stream or fluidizing medium, is heated in the reactor by the heat of polymerization. This heat is removed from the recycle composition in another part of the cycle by a cooling system external to the reactor.
  • a gas fluidized bed process for producing polymers a gaseous stream containing one or more monomers is continuously cycled through a fluidized bed in the presence of a catalyst under reactive conditions. The gaseous stream is withdrawn from the fluidized bed and recycled back into the reactor. Simultaneously, polymer product is withdrawn from the reactor and fresh monomer is added to replace the polymerized monomer.
  • the reactor pressure in a gas phase process may vary from about 100 psig (690 kPa) to about 500 psig (3448 kPa), preferably in the range of from about 200 psig (1379 kPa) to about 400 psig (2759 kPa), more preferably in the range of from about 250 psig (1724 kPa) to about 350 psig (2414 kPa).
  • the reactor temperature in a gas phase process may vary from about 30°C to about 120°C, preferably from about 60°C to about 115°C, more preferably in the range of from about 70°C to 110°C, and most preferably in the range of from about 70°C to about 95°C.
  • the reactor utilized in the present invention is capable and the process of the invention is producing greater than 500 lbs of polymer per hour (227 Kg/hr) to about 200,000 lbs/hr (90,900 Kg/hr) or higher of polymer, preferably greater than 1000 lbs/hr (455 Kg/hr), more preferably greater than 10,000 lbs/hr (4540 Kg/hr), even more preferably greater than 25,000 lbs/hr (11,300 Kg/hr), still more preferably greater than 35,000 lbs/hr (15,900 Kg/hr), still even more preferably greater than 50,000 lbs/hr (22,700 Kg/hr) and most preferably greater than 65,000 lbs/hr (29,000 Kg/hr) to greater than 100,000 lbs/hr (45,500 Kg/hr).
  • a slurry polymerization process generally uses pressures in the range of from about 1 to about 50 atmospheres and even greater and temperatures in the range of 0°C to about 120° C.
  • a suspension of solid, particulate polymer is formed in a liquid polymerization diluent medium to which ethylene and comonomers and often hydrogen along with catalyst are added.
  • the suspension including diluent is intermittently or continuously removed from the reactor where the volatile components are separated from the polymer and recycled, optionally after a distillation, to the reactor.
  • the liquid diluent employed in the polymerization medium is typically an alkane having from 3 to 7 carbon atoms, preferably a branched alkane.
  • the medium employed should be liquid under the conditions of polymerization and relatively inert.
  • a propane medium When used the process must be operated above the reaction diluent critical temperature and pressure.
  • a hexane or an isobutane medium is employed.
  • a preferred polymerization technique of the invention is referred to as a particle form polymerization, or a slurry process where the temperature is kept below the temperature at which the polymer goes into solution.
  • a particle form polymerization or a slurry process where the temperature is kept below the temperature at which the polymer goes into solution.
  • Such technique is well known in the art, and described in for instance U.S. Patent No. 3,248,179 which is fully incorporated herein by reference.
  • Other slurry processes include those employing a loop reactor and those utilizing a plurality of stirred reactors in series, parallel, or combinations thereof.
  • Non-limiting examples of slurry processes include continuous loop or stirred tank processes.
  • other examples of slurry processes are described in U.S. Patent No. 4,613,484 .
  • the reactor used in the slurry process of the invention is capable of and the process of the invention is producing greater than 2000 lbs of polymer per hour (907 Kg/hr), more preferably greater than 5000 lbs/hr (2268 Kg/hr), and most preferably greater than 10,000 lbs/hr (4540 Kg/hr).
  • the slurry reactor used in the process of the invention is producing greater than 15,000 lbs of polymer per hour (6804 Kg/hr), preferably greater than 25,000 lbs/hr (11,340 Kg/hr) to about 100,000 lbs/hr (45,500 Kg/hr).
  • a preferred process of the invention is where the process, preferably a slurry or gas phase process is operated in the presence of a bulky ligand metallocene-type catalyst system of the invention and in the absence of or essentially free of any scavengers, such as triethylaluminum, trimethylaluminum, tri-isobutylaluminum and tri-n-hexylaluminum and diethyl aluminum chloride, dibutyl zinc and the like.
  • any scavengers such as triethylaluminum, trimethylaluminum, tri-isobutylaluminum and tri-n-hexylaluminum and diethyl aluminum chloride, dibutyl zinc and the like.
  • the process is operated by introducing a benzil compound into the reactor and/or contacting a benzil compound with the bulky ligand metallocene-type catalyst system of the invention prior to its introduction into the reactor.
  • the polymers produced by the process of the invention can be used in a wide variety of products and end-use applications.
  • the polymers produced by the process of the invention include linear low density polyethylene, elastomers, plastomers, high density polyethylenes, low density polyethylenes, polypropylene and polypropylene copolymers.
  • the polymers typically ethylene based polymers, have a density in the range of from 0.86g/cc to 0.97 g/cc, preferably in the range of from 0.88 g/cc to 0.965 g/cc, more preferably in the range of from 0.900 g/cc to 0.96 g/cc, even more preferably in the range of from 0.905 g/cc to 0.95 g/cc, yet even more preferably in the range from 0.910 g/cc to 0.940 g/cc, and most preferably greater than 0.915 g/cc to about 0.930 g/cc.
  • melt strength of the polymers produced using the catalyst of the invention are greater than 4 cN, preferably greater than 5 cN.
  • melt strength is measured with an Instron capillary rheometer in conjunction with the Goettfert Rheotens melt strength apparatus.
  • a polymer melt strand extruded from the capillary die is gripped between two counter-rotating wheels on the apparatus.
  • the take-up speed is increased at a constant acceleration of 24 mm/sec 2 , which is controlled by the Acceleration Programmer (Model 45917, at a setting of 12).
  • the maximum pulling force (in the unit of cN) achieved before the strand breaks or starts to show draw-resonance is determined as the melt strength.
  • the temperature of the rheometer is set at 190°C.
  • the capillary die has a length of one inch (2.54 cm) and a diameter of 0.06" (0.1 5cm).
  • the polymer melt is extruded from the die at a speed of 3 inch/min (7.62 cm/min).
  • the distance between the die exit and the wheel contact point should be 3.94 inches (100 mm).
  • the polymers produced by the process of the invention typically have a molecular weight distribution, a weight average molecular weight to number average molecular weight (M w /M n ) of greater than 1.5 to about 15, particularly greater than 2 to about 10, more preferably greater than about 2.5 to less than about 8, and most preferably from 3.0 to 8.
  • M w /M n weight average molecular weight to number average molecular weight
  • the polymers of the present invention have a M z /M w of greater than or equal to 3, preferably greater than 3.
  • M z is the z-average molecular weight.
  • the polymers of the invention have a M z /M w of greater than or equal to 3.0 to about 4.
  • the M z /M w is in the range greater than 3 to less than 4.
  • the polymers of the invention typically have a narrow composition distribution as measured by Composition Distribution Breadth Index (CDBI). Further details of determining the CDBI of a copolymer are known to those skilled in the art. See, for example, PCT Patent Application WO 93/03093, published February 18, 1993 , which is fully incorporated herein by reference.
  • CDBI Composition Distribution Breadth Index
  • the bulky ligand metallocene-type catalyzed polymers of the invention in one embodiment have CDBI's generally in the range of greater than 50% to 100%, preferably 99%, preferably in the range of 55% to 85%, and more preferably 60% to 80%, even more preferably greater than 60%, still even more preferably greater than 65%.
  • polymers produced using a bulky ligand metallocene-type catalyst system of the invention have a CDBI less than 50%, more preferably less than 40%, and most preferably less than 30%.
  • the polymers of the present invention in one embodiment have a melt index (MI) or (I 2 ) as measured by ASTM-D-1238-E in the range from 0.01 dg/min to 1000 dg/min, more preferably from about 0.01 dg/min to about 100 dg/min, even more preferably from about 0.1 dg/min to about 50 dg/min, and most preferably from about 0.1 dg/min to about 10 dg/min.
  • MI melt index
  • I 2 melt index
  • the polymers of the invention in an embodiment have a melt index ratio (I 21 /I 2 ) (I 21 is measured by ASTM-D-1238-F) of from 30 to less than 200, more preferably from about 35 to less than 100, and most preferably from 40 to 95.
  • I 21 is measured by ASTM-D-1238-F
  • the polymers of the invention in a preferred embodiment have a melt index ratio (I 21 /I 2 ) (I 21 is measured by ASTM-D-1238-F) of from preferably greater than 30, more preferably greater than 35, even more preferably greater that 40, still even more preferably greater than 50 and most preferably greater than 65.
  • the polymers of the invention may be blended and/or coextruded with any other polymer.
  • Non-limiting examples of other polymers include linear low density polyethylenes produced via conventional Ziegler-Natta and/or bulky ligand metallocene-type catalysis, elastomers, plastomers, high pressure low density polyethylene, high density polyethylenes, polypropylenes and the like.
  • Polymers produced by the process of the invention and blends thereof are useful in such forming operations as film, sheet, and fiber extrusion and co-extrusion as well as blow molding, injection molding and rotary molding.
  • Films include blown or cast films formed by coextrusion or by lamination useful as shrink film, cling film, stretch film, sealing films, oriented films, snack packaging, heavy duty bags, grocery sacks, baked and frozen food packaging, medical packaging, industrial liners, membranes, etc. in food-contact and non-food contact applications.
  • Fibers include melt spinning, solution spinning and melt blown fiber operations for use in woven or non-woven form to make filters, diaper fabrics, medical garments, geotextiles, etc.
  • Extruded articles include medical tubing, wire and cable coatings, geomembranes, and pond liners. Molded articles include single and multi-layered constructions in the form of bottles, tanks, large hollow articles, rigid food containers and toys, etc.
  • methylalumoxane (MAO) used was a 30 weight percent MAO solution in toluene (typically 13.5 wt% Aluminum and 28.2 wt% MAO by NMR) available from Albemarle Corporation, Baton Rouge, Louisiana, the Davison 948 silica dehydrated to 600 °C (silica gel) available from W.R. Grace, Davison Chemical Division, Baltimore, Maryland. Toluene was anhydrous from Aldrich, and used without further purification.
  • the compounds (C 3 H 6 )SiCl 2 and (C 4 H 8 )SiCl 2 were purchased from Gelest and Lancaster.
  • Example 1 illustrates the typical synthesis route to producing the compounds of the invention including those used in the following examples.
  • All the catalysts prepared in Examples 2 through 8 were screened in a fluidized bed reactor equipped with devices for temperature control, catalyst feeding or injection equipment, GC analyzer for monitoring and controlling monomer and gas feeds and equipment for polymer sampling and collecting.
  • the reactor consists of a 6 inch (15.24 cm) diameter bed section increasing to 10 inches (25.4 cm) at the reactor top. Gas comes in through a perforated distributor plate allowing fluidization of the bed contents and polymer sample is discharged at the reactor top.
  • reaction mixture was heated to 155° F (68.3° C) and stirred for 1 hr.
  • the reaction mixture was transferred to a large glass flask and 500 g silica gel was added with mixing. Two additional increments of silica gel (250 g each) were added to the mixture.
  • the supported catalyst was added back to the original reactor vessel with stirring and 28.6 g AS-990 in 286 ml of toluene was added.
  • AS-990 is (N,N-bis (2-hydroxylethyl)octadecylamine (C 18 H 37 N(CH 2 CH 2 OH) 2 )) available as Kemamine AS-990 from ICI Specialties, Wilmington, Delaware).
  • the catalyst was dried by N 2 purge at 120° F (49 °C) until free flowing.
  • the dried catalyst was dry-mixed with 3.0 wt% of Aluminum Stearate #22 in a dry box, (AlSt #22 is (CH 3 (CH 2 ) 16 COO) 2 Al-OH and is available from Witco Corporation, Memphis, Tennessee), then transferred to a catalyst bomb for testing.
  • 1609 ml of 30% MAO in toluene (available from Albemarle Corporation, Baton Rouge, Louisiana) was added to a 2 gallon glass reactor vessel with a heating/cooling jacket and a helical ribbon blender having a central auger-type shaft. 2200 ml toluene was added to the reaction vessel. A suspension of 19.4 g (C 3 H 6 Si(C 5 H 4 )(C 5 Me 4 )ZrF 2 in 250 ml toluene was transferred to the reaction vessel via cannula. An additional 200 ml toluene was used to rinse the bottle containing the metallocene compound suspension. The reaction mixture was heated to 155° F (68.3° C) and stirred for 1 hr.
  • reaction mixture was transferred to a large glass flask and 500 g silica gel was added with mixing. Two additional increments of silica gel (250 g each) were added to the mixture.
  • the supported catalyst was added back to the original reactor vessel with stirring and 30.2 g AS-990 in 286 ml of toluene was added.
  • AS-990 is (N,N-bis (2-hydroxylethyl) octadecylamine (C 18 H 37 N(CH 2 CH 2 OH) 2 )) available as Kemamine AS-990 from ICI Specialties, Wilmington, Delaware).
  • the catalyst was dried by N 2 purge at 120° F (49°C) until free flowing.
  • the dried catalyst was dry-mixed with 2.5 wt% of Aluminum Stearate #22 in a dry box, (AlSt #22 is (CH 3 (CH 2 ) 16 COO) 2 Al-OH and is available from Witco Corporation, Memphis, Tennessee), then transferred to a catalyst bomb for testing.
  • 1609 ml of 30% MAO in toluene (available from Albemarle Corporation, Baton Rouge, Louisiana) was added to a 2 gallon glass reactor vessel with a heating/cooling jacket and a helical ribbon blender having a central auger-type shaft. 2200 ml toluene was added to the reaction vessel. A suspension of 22.04 g (C 4 H 8 )Si(C 5 Me 4 )(C 5 H 4 )ZrCl 2 in 250 ml toluene was transferred to the reaction vessel via cannula. An additional 200 ml toluene was used to rinse the bottle containing the metallocene compound suspension.
  • reaction mixture was heated to 155° F (68.3° C) and stirred for 1 hr.
  • the reaction mixture was transferred to a large glass flask and 500 g silica gel was added with mixing. Two additional increments of silica gel (250 g each) were added to the mixture.
  • the supported catalyst was added back to the original reactor vessel with stirring and 30.2 g AS-990 in 286 ml of toluene was added.
  • AS-990 is (N,N-bis (2-hydroxylethyl) octadecylamine (C 18 H 37 N(CH 2 CH 2 OH) 2 )) available as Kemamine AS-990 from ICI Specialties, Wilmington, Delaware).
  • the catalyst was dried by N 2 purge at 120° F (49°C) until free flowing.
  • the dried catalyst was dry-mixed with 2.5 wt% of Aluminum Stearate #22 in a dry box, (AlSt #22 is (CH 3 (CH 2 ) 16 COO) 2 Al-OH and is available from Witco Corporation, Memphis, Tennessee), then transferred to a catalyst bomb for testing.
  • the catalyst systems of the Examples above were then tested in a continuous gas phase fluidized bed reactor which comprised a nominal 18 inch (45.7cm), schedule 60 reactor having an internal diameter of 16.5 inches (41.9cm).
  • the fluidized bed is made up of polymer granules.
  • the gaseous feed streams of ethylene and hydrogen together with liquid comonomer were mixed together in a mixing tee arrangement and introduced below the reactor bed into the recycle gas line. Hexene-1 was used as the comonomer.
  • the individual flow rates of ethylene, hydrogen and comonomer were controlled to maintain fixed composition targets.
  • the ethylene concentration was controlled to maintain a constant ethylene partial pressure.
  • the hydrogen was controlled to maintain a constant hydrogen to ethylene mole ratio.
  • the concentration of all the gases were measured by an on-line gas chromatograph to ensure relatively constant composition in the recycle gas stream.
  • the catalyst system was injected directly into the fluidized bed using purified nitrogen as a carrier. Its rate was adjusted to maintain a constant production rate.
  • the reacting bed of growing polymer particles is maintained in a fluidized state by the continuous flow of the make up feed and recycle gas through the reaction zone. A superficial gas velocity of 1-3 ft/sec (31-91 cm/sec) was used to achieve this.
  • the reactor was operated at a total pressure of 300 psig (2069 kPa). To maintain a constant reactor temperature, the temperature of the recycle gas is continuously adjusted up or down to accommodate any changes in the rate of heat generation due to the polymerization.
  • the fluidized bed was maintained at a constant height by withdrawing a portion of the bed at a rate equal to the rate of formation of particulate product.
  • the product is removed semi-continuously via a series of valves into a fixed volume chamber, which is simultaneously vented back to the reactor. This allows for highly efficient removal of the product, while at the same time recycling a large portion of the unreacted gases back to the reactor.
  • This product is purged to remove entrained hydrocarbons and treated with a small steam of humidified nitrogen to deactivate any trace quantities of residual catalyst.
  • the properties of the polymer were determined by the following test methods: Property Units Procedure Melt Indices, Melt Flow Ratios dg/min ASTM D- 1238 Density g/cc ASTM D-1505 Haze % ASTM D-1003 Gloss @ 45° % ASTM D-2457 Tensile @ Yield mPa ASTM D-882 Elongation @ Yield % ASTM D-882 Tensile @ Break mPa ASTM D-882 Elongation @ Break % ASTM D-882 1% Secant Modulus mPa ASTM D-882 Dart Drop Impact g/ ⁇ m ASTM D-1709 (A) Elmendorf Tear Resistance g/ ⁇ m ASTM D-1922 Melt Strength cN As described in Specification Composition Distribution Breadth Index % As described in Specification Composition Distribution Breadth Index % As described in Specification Composition Distribution Breadth Index % As described in Specification Composition Distribution Breadth Index % As described in Specification Composition Distribution Breadth Index % As described in
  • the polymers and the films produced therefrom of the present invention were produced using the cyclic bridged metallocene-type catalyst systems of the invention.
  • the cyclic bridged metallocene catalyst compounds used were as follows: Catalyst A is cyclotrimethylenesilyl(tetramethyl cyclopentadienyl) (cyclopentadienyl) zirconium dichloride, Catalyst B is cyclotetramethylenesilyl(tetramethyl cyclopentadienyl) (cyclopentadienyl) zirconium dichloride, and Catalyst C is cyclotrimethylenesilyl (tetramethyl cyclopentadienyl) (2-methyl indenyl) zirconium dichloride, Catalyst D is cyclotrimethylenesilyl(tetramethyl- cyclopentadienyl) (3-methyl cyclopentadienyl) zirconium dichloride,
  • Table 3 includes the data generated using a catalyst of the invention in a gas phase polymerization process similar to that described in Example 14 to produce an ethylene/hexene-1 copolymer.
  • Table 3A below gives film data for the polymers described in Table 3 in Examples 14 through 18.
  • Table 4 includes the data generated using a catalyst of the invention in a gas phase polymerization process similar to that described in Example 9 to produce an ethylene/hexene-1 copolymer.
  • Example 14 15 16 17 18 19 20 Catalyst Used C C A A B B B Density (g/cc) 0.9196 0.9219 0.9221 0.9175 0.9178 0.9186 0.9250 Melt Index (g/10 min) 0.90 2.06 0.74 0.86 0.92 2.16 1.27 Melt Index Ratio (I 21 /I 2 ) 36 46 100 77 70 58 68 Melt Strng. (cN) 6.5 4.4 6.2 5.9 4.0 4.3 4.4 Melting Peaks 1 st M.P.
  • alumoxane is combined with the transition metal complex in toluene to form a precursor solution.
  • a porous support is added with vigorous mixing until the material is no longer mobile. The remaining support is added at this point and the mixture is thoroughly homogenized with a spatula.
  • the total volume of the precursor solution is greater than the pore volume of the support, about 100% - 200% pore volume, but not enough to reach the point of gelation or form a slurry.
  • the solvent is removed in vacuo and ambient temperature for about 12 to 16 hours.
  • the catalyst preparations are summarized in Table 5.
  • the catalyst mixtures are prepared by weighing out the appropriate supported catalyst components into a glass vessel and shaking the mixture until it is homogeneous.
  • the alumoxane used is 30 wt.% methyl alumoxane in toluene available from Albemarle Corporation, Baton Rouge, Louisiana.
  • the toluene is air and moisture free (Aldrich anhydrous grade) and is stored over molecular sieves.
  • Table 5 includes information on the synthesis of these catalysts. Table 5 Ex. Cat used Cat (mg) Cat ( ⁇ mol) MAO (g) Tol. (g) SiO 2 (g) TM+ ⁇ mol/g support P.V.
  • a continuous cycle fluidized bed gas phase polymerization reactor is used for the polymerization studies summarized in Tables 6 and 7.
  • the reactor is equipped with devices for temperature and pressure control, catalyst and gas feed injection, GC analyzer for monitoring and controlling monomer and gas feeds, and polymer sampling and collecting.
  • the reactor consists of a 6" diameter bed section increasing to 10" at the reactor top. Gas enters through a perforated distributor plate allowing fluidization of the bed contents and polymer is discharged at the reactor top. Polymer samples are collected after several bed turnovers once the reactor and product are stabilized.
  • the polymerizations carried out were in the presence of catalysts mixtures, the catalysts being described in Table 5.
  • a the cyclic bridged metallocene-type catalyst compound of the invention can be combined with one or more non-cyclic bridged metallocene-type catalyst compounds.
  • the process of the invention may be used in a series reactor polymerization process. For example, a supported cyclic bridged bulky ligand metallocene-type catalyst compound is used in one reactor and a non-cyclic bridged or unbridged, bulky ligand metallocene-type catalyst compound being used in another or vice-versa.

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Claims (3)

  1. Procédé de polymérisation d'oléfine(s) pour produire un produit polymère en présence d'un système de catalyseur comprenant un composé catalyseur de type métallocène à ligand volumineux ponté cyclique achiral et un activateur, dans lequel le composé catalyseur de type métallocène à ligand volumineux ponté cyclique achiral est représenté par la formule :

            LA(R'AxR')LBMQn     (I)

    dans laquelle M représente un métal de transition du groupe 4, 5, 6, LA et LB représentent un ligand cyclopentadiényle ou un ligand de type cyclopentadiényle volumineux, non substitué ou substitué, lié à M ; (R'AxR') est un groupe pontant cyclique dans lequel A représente un ou plusieurs, ou une combinaison, d'atomes de carbone, de germanium, de silicium ou d'étain pontant LA et LB, et les deux radicaux R' forment un noyau ou système de noyau cyclique avec A ; indépendamment, chaque radical Q représente un ligand mono-anionique, ou éventuellement deux radicaux Q forment ensemble un ligand chélateur anionique divalent ; et dans laquelle n est égal à 0, 1 ou 2 suivant l'état d'oxydation formel de M, et x représente un nombre entier de 1 à 4 et dans laquelle le composé catalyseur de type métallocène à ligand volumineux ponté cyclique achiral selon (I) n'est pas le composé représenté par la formule (II)
    Figure imgb0013
     dans laquelle R1 et R2 sont choisis chacun dans le groupe constitué par un groupe alkyle, un groupe aryle et un groupe alkyle contenant du silicium ; M représente un métal choisi dans le groupe IV du tableau périodique ; Q représente un atome de carbone ou de silicium ; X représente un halogène, un groupe alkyle ou un ligand anionique, et ils peuvent être choisis de manière à être identiques ou à être une combinaison de groupes différents ; i représente un nombre entier de 1 à 10 ; n représente un nombre entier de 1 à 4 ; m représente un nombre entier de 0 à 4 ; et h représente un nombre entier de 1 à 3.
  2. Procédé selon la revendication 1 dans lequel un des groupes LA ou LB est un ligand cyclopentadiényle substitué ou un ligand volumineux de type cyclopentadiényle substitué.
  3. Procédé selon la revendication 1 dans lequel le système de catalyseur est supporté.
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EP1624000A1 (fr) 2006-02-08
ATE517130T1 (de) 2011-08-15
JP2002544296A (ja) 2002-12-24
AU763151B2 (en) 2003-07-17
BR0010679A (pt) 2003-07-22
AU4246400A (en) 2000-11-21
EP1189951A1 (fr) 2002-03-27
US20020058828A1 (en) 2002-05-16
US6339134B1 (en) 2002-01-15
CA2372636A1 (fr) 2000-11-16
WO2000068279A1 (fr) 2000-11-16
DE60024085D1 (de) 2005-12-22
JP3607615B2 (ja) 2005-01-05
ES2253219T3 (es) 2006-06-01
DE60024085T2 (de) 2006-08-03
EP1189951B1 (fr) 2005-11-16
US6388115B1 (en) 2002-05-14

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